Underground reactor system

ABSTRACT

An underground reactor for creating hydrocarbons and chemicals from organic material can include a heat recovery device. Some embodiments of the present disclosure include at least one tube that injects biomass underground and at least one second tube that collects reacted biomass on the surface. Further tubes are also disclosed for the ability to control temperature and pressure and collect minerals and carbon dioxide. In another embodiment, a super-critical fluid is injected into the underground reactor. Methods for utilizing the reactor are additionally provided. Further embodiments include methods of using the reactor such as, for example, methods of creating fuel from algae and methods of using the minerals and carbon dioxide as food for an algae farm that will be used as biomass for the reactor.

RELATED APPLICATIONS

This application claims priority to U.S. Provisional Application 61/681,850 filed Aug. 10, 2012.

CROSS-REFERENCE TO RELATED APPLICATIONS

U.S. Provisional Patent Application Ser. No. 61/481,918, filed 3 May 2011, U.S. Provisional Patent Application Ser. No. 61/602,841, filed 24 Feb. 2012, and PCT Application No. PCT/US2012/036400, all are hereby incorporated herein by reference.

BACKGROUND

As the world population continues to increase, more sustainable energy processes must be used to support more people. Many oil wells have been drilled around the globe to pump oil from the ground and then are abandoned once the well runs dry.

Meanwhile, biofuels has begun a completely separate track of development, where conversion of biomass to alcohol-based fuels are the primary focus.

Significant research and development into algae and diatoms began in 1978, due to the Organization of the Petroleum Exporting Countries (OPEC) oil embargo. Prior to 1978 Jack Myers and Bessel Kok published a book on Algal Culture “From Laboratory to Pilot Plant” and Massachusetts Institute of Technology (MIT) had mass culture projects on the rooftop circa 1950. Research ramped up when the Department of Energy's (DOE) Office of Fuels Development funded the original Aquatic Species Program (ASP) at the National Renewable Energy Laboratory (NREL) for 16 years to define and determine the industrial viability of algae to energy. The 1998 ASP close-out report identifies green algae and diatoms as the most primitive forms of plants, thus most efficient at cell division and growth because they do not waste energy on infrastructure, such as roots, stems and leaves as terrestrial plants do. The ASP concluded that because of microalgae's primitive nature, oil yields were estimated at 30 times more per unit area of land for microalgae than terrestrial oil-seed crops. However, the focus of the ASP report was on making biodiesel from algae lipids, not synthetic crude oil.

The 1998 ASP close-out report emphasizes critical open algae pond issues, stemming from the inability to maintain consistently high algae biomass growth rates due to uncontrollable temperature changes in the weather and seasons.

Additionally, it stated that there is little prospect for alternative industrial scale production of algae without using the open algae pond designs.

Further, algae production cost analysis was recommended due to the difficulty of maintaining highly productive organisms. Algae biomass production rate is determined by the availability of nutrients, intensity of light, temperature and CO₂. The effect of light, nutrients and temperature are multiplicative.

Calculations have been done indicating the temperatures and pressures required for a reaction to occur. As relative permittivity decreases, water acts more as a solvent, partially attributable to reduced polarity. Using the Arrhenius equation, water dissociation constant has been calculated for variable temperature and constant pressure, or variable pressure and constant temperature.

Thermal spallation is a process that applies significant heat flux to hard rock. The rapid stress causes surface grains to break away from rock in a process known in the art as spallation, which uses super-heated fluid to dissolve the rock.

Incorporated herein by reference are the following references:

-   U.S. Pat. No. 4,003,393 (which discloses a dissolvable pipeline     pig). -   U.S. Pat. No. 4,467,861; AU 2011200090 (A1); US2011/092726;     WO2009149519A1; U.S. Pat. No. 3,955,317; U.S. Pat. No. 5,958,761;     FR2564855; EP1923460; EP1382576; US2005/064577; DE102006045872;     US2004/033557; US2007/295505; U.S. Pat. No. 6,468,429; WO2011086358;     GB2473865; DE102006045872; US2004/0033557; US2007/0295505; U.S. Pat.     No. 4,937,052; U.S. Pat. No. 4,272,383; U.S. Pat. No. 7,866,385;     U.S. Pat. No. 7,977,282. -   Modeling Algae Growth in an Open-Channel Raceway by Scott C. James     and Varun Boriah. -   Advanced Organic Rankine Cycles in Binary Geothermal Power Plants by     Uri Kaplan, World Energy Council, 2007. -   Hydrothermal Liquifaction to Convert Biomass into Crude Oil by     Yuanhui Zhang, ch. 10, Biofuels from Agricultural Wastes and     Byproducts, 2010. -   Biomass gasification in near- and super-critical water: Status and     Prospects by Yukihiko Matsumara, et al., Biomass and Bioenergy,     2005. -   Organic Rankine Cycle Configurations by Uri Kaplan, Proceedings     European Geothermal Congress, 2007. -   Utilizing Organic Rankine Cycle Turbine Systems to Efficiently Drive     Field Injection Pumps by Nadav Amir, GRC2007 Annual Meeting, 2007. -   ASME Steam Tables. Thermodynamic and Transport Properties of Steam,     The 1967 IFC formulation for industrial use. 6th Edition, ASME,     1993. -   Benjamin, M. 2002. Water Chemistry, 1st edition. New York: McGraw     Hill. -   Aqueous Systems at Elevated Temperatures and Pressures: Physical     Chemistry in Water, Steam and Hydrothermal Solutions, International     Association for the Properties of Water and Steam, 2004. -   Piezoelectricity: History and New Thrusts, Ultrasonics Symposium,     1996.

Adiabatic Processes http://hyperphysics.phy-astr.gsu.edu/hbase/thermo/adiab.html, Georgia State University

-   Manual on Harmful Marine Microalgae edited by G. M.     Hallegraeff, D. M. Anderson & A. D. Cembella, IOC Manuals and Guides     No. 33, UNESCO, 1995. -   Media for the Culture of Oceanic Ultraphytoplankton by M. Keller, R.     Selvin, W. Claus & R. Guillard, Journal of Phycology Vol. 23, April     2007. -   Affordable Low Carbon Diesel from Domestic Coal and Biomass by     Tarka, Thomas J.; Wimer, John G.; Balash, Peter C.; Skone, Timothy     J.; Kern, Kenneth C.; Vargas, Maria C.; Morreale, Bryan D.; White     III, Charles W.; & Gray, David, United States Department of Energy,     National Energy Technology Laboratory. p. 21. (2009). -   Coal liquefaction: The chemistry and technology of thermal processes     Whitehurst, D. D.; Mitchell, T. O.; Farcasiu, M. New York, Academic     Press, Inc., 1980.

SUMMARY

An embodiment of the disclosure includes an underground reactor for use in creating fuel from organic material, comprising: a first conduit that injects an organic material underground; a second conduit that collects reacted organic material produced by the underground reactor; a heat exchanger for extracting heat; a biomass source; and concentrating equipment that separates the biomass from its cultivation medium. Another embodiment comprises further comprising a plurality of capillary injection tubes. In another embodiment the heat exchanger is used for powering equipment used in the fuel creation process. In yet another embodiment the concentrating equipment is a centrifuge. Yet another embodiment comprises an expander powered by geothermal energy. In an embodiment, the expander is a turbine. In still another embodiment, the expander powers the concentrating equipment. In still another embodiment, the biomass source is a biomass farm that grows the organic material.

In an embodiment of the underground reactor for use in creating hydrocarbons, from organic material, comprises a first conduit that injects an organic material underground; a second conduit that collects reacted organic material produced by the underground reactor; and a heat exchanger for extracting heat; wherein the organic material is pulverized coal. In an embodiment, the underground reactor comprises a plurality of capillary injection tubes. In an embodiment, the heat exchanger is used for powering equipment used in the fuel creation process.

An embodiment includes a method of performing a high-pressure, high-temperature reaction comprising: sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals; bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit; using a heat exchanger for extracting heat; and sending geothermal fluid to a biomass growth. In an embodiment, the geothermal fluid comprises carbonates and biocarbonates. In an embodiment, super-critical fluid is injected through capillary tubes in the first conduit. In an embodiment, the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, or chemicals.

An embodiment of the disclosure includes a method of performing a high-pressure, high-temperature reaction comprising: sending biomass underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals; bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit; using a heat exchanger for extracting heat; and circulating fluid in a closed loop to keep the biomass growth at a desired temperature. In an embodiment, super-critical fluid is injected through capillary tubes in the first conduit. In another embodiment, the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, or chemicals.

In an embodiment, a method of performing a high-pressure, high-temperature reaction comprises: separating biomass from its cultivation medium; sending the biomass underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals; bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit; and using a heat exchanger for extracting heat. In another embodiment, super-critical fluid is injected through capillary tubes in the first conduit. In yet another embodiment, the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals. In still another embodiment, the cultivation medium is water. In another embodiment, the water is separated from the biomass using geothermal heat. In an embodiment, the biomass is separated from its cultivation medium using concentrating equipment. In yet another embodiment, the concentrating equipment is at least one centrifuge. In yet another embodiment, skimming equipment is used for dewatering. In an embodiment, geothermal energy is used to power the concentrating equipment. In an embodiment, the geothermal energy is harnessed through at least one expander. In an embodiment, the expander is a turbine. An embodiment of the present disclosure includes adjusting the reactor temperature by a method selected from the group consisting of increasing pump-around flow rate, decreasing pump-around flow rate, increasing tubular reactor flow rate, decreasing tubular reactor flow rate, increasing tubular reactor inlet temperature, increasing super critical fluid (SCF) flow, decreasing SCF flow, changing SCF medium, increasing SCF temperature, decreasing SCF temperature, increasing SCF pressure, decreasing SCF pressure, independently adjusting SCF pressure, temperature, flow and medium within each injection tube or capillary, decreasing tubular reactor inlet temperature, increasing pump-around re-injection temperature, and decreasing pump-around re-injection temperature.

Some embodiments of the disclosure include an underground hydro-geothermal reactor that converts renewable and carbonaceous feedstocks to fuel via temperature and pressure. Embodiments of the reactor can utilize produced coke and off gas to generate electricity and heat, produced carbon dioxide and heated mineral-rich water to enhance biomass growth.

Some embodiments use algae as the biomass feedstock as well as lignite, bitumen, and coal as carbonaceous feedstock. Other embodiments have open or closed autotrophic, mixotrophic or heterotrophic algae cultivation production systems near the reactor that are used for feedstock. Some embodiments utilize effluent water to provide temperature control for algae raceway ponds by using indirect geothermal energy. Further embodiments allow for the reactor's recycle streams to provide nitrogen, phosphorous, potassium, carbon dioxide, and elevated temperature in open algae ponds. The present disclosure includes an underground reactor for use in a fuel creation process for creating fuel from organic material, comprising a first tube that injects an organic material underground; In an embodiment a second tube that collects reacted organic material produced by the underground reactor; a heat exchanger for extracting heat to be used in powering equipment used in the fuel creation process.

In an embodiment, the present disclosure further comprises an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the fuel creation process. In an embodiment, the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger. In an embodiment, the equipment includes a pump. In an embodiment, the pump circulates heat exchange fluid to keep a reaction zone at a desired temperature.

The present disclosure includes an underground reactor for use in a fuel creation process for creating fuel from organic material, comprising a first tube that injects an organic material underground; a second tube that collects reacted organic material produced by the underground reactor; and a pump which circulates heat exchange fluid in a closed loop to keep a reaction zone at a desired temperature. In an embodiment, the present disclosure further comprises a heat exchanger for extracting heat to be used in powering equipment used in the fuel creation process. In an embodiment, the present disclosure further comprises an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the fuel creation process. In an embodiment, the equipment includes the pump. In an embodiment, the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger. In an embodiment, the organic material is biomass. In an embodiment, the biomass is algae. In an embodiment, the organic material is a polymer. In an embodiment, the organic material is carbonaceous, such as lignite, bitumen or coal. In an embodiment, the organic material is pulverized coal. In an embodiment, the organic material is solid waste.

In an embodiment, the organic material is reacted through liquefaction. In an embodiment, the organic material is reacted through a thermochemical reaction. In an embodiment, the organic material is reacted through hydrothermal processes.

In an embodiment, the second tube is within the first tube. In an embodiment, the first tube is closed at its bottom and the second tube is open at its bottom. In an embodiment, the first tube is deeper underground than the second tube. In an embodiment, the present disclosure further comprises a casing that encloses the first tube and the second tube. In an embodiment, the casing goes at least as deep as the first tube. In an embodiment, the casing does not go as deep as the first tube. In an embodiment, the present disclosure further comprises a screen that goes down to the depth of the first tube. In an embodiment, the casing is an insulator. In an embodiment, the insulator is cement.

In an embodiment, the present disclosure further comprises at least a third tube that a heat transfer material can be pumped through. In an embodiment, the heat transfer material is water. In an embodiment, the present disclosure further comprises an oil, gas, solids, and water separator that separates the products effluent from the reactor. In an embodiment, the separator is above ground. In an embodiment, the separator is below ground.

In an embodiment, a portion of the products are stored. In an embodiment, a portion of the products are used as food to grow biomass. In an embodiment, a portion of the products as used to generate electricity. In an embodiment, electricity is generated via a heat exchange. In an embodiment, at least the first tube is curved. In an embodiment, at least the first tube is sloped. In an embodiment, at least the first tube forks.

The present disclosure includes a method of performing a high-pressure, high-temperature reaction comprising sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to fuel, hydrocarbon, or chemicals; bringing the fuel, hydrocarbon, or chemicals up through a second conduit; and circulating heat exchange fluid in a closed loop to keep the reaction zone at a desired temperature.

In an embodiment, the present disclosure further comprises using a heat exchanger for extracting heat to be used in powering equipment used in the conversion process. In an embodiment, the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger. In an embodiment, the present disclosure further comprises using an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the conversion process. In an embodiment, the equipment includes the pump.

The present disclosure includes a method of performing a high-pressure, high-temperature reaction comprising: sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to fuel, hydrocarbon, or chemicals; bringing the fuel, hydrocarbon, or chemicals up through a second conduit; and using a heat exchanger for extracting heat to be used in powering equipment used in the conversion process.

In an embodiment, the present disclosure further comprises circulating heat exchange fluid in a closed loop to keep the reaction zone at a desired temperature.

In an embodiment, the present disclosure further comprises using an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the conversion process.

In an embodiment, the equipment includes the pump. In an embodiment, the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

In an embodiment, pressure can be adjusted by increasing or decreasing tubular reactor depth or increasing or decreasing back pressure at surface or loading the tubular reactor working fluid with high specific gravity material mixed within the working fluid.

In an embodiment, the present disclosure further comprises sending a heat transfer material underground. In an embodiment, the present disclosure further comprises controlling the temperature of the heat transfer material by adjusting circulation rate. In an embodiment, the present disclosure further comprises controlling the temperature of the heat transfer material by increasing or decreasing the temperature of the organic material. In an embodiment, the present disclosure further comprises frac'ing the rock prior to sending the heat transfer material underground. In an embodiment, the present disclosure further comprises sending the heat transfer material from underground into a heat exchanger. In an embodiment, the present disclosure further comprises sending the heat transfer material from underground into an organic rankine cycle.

In an embodiment, the present disclosure further comprises separating the products into oil, gas and water-based solution. In an embodiment, the present disclosure further comprises sending the water-based solution to a biomass growth. In an embodiment, the present disclosure further comprises pumping the fluid out of the ground and sending it to a biomass growth facility or farm.

In an embodiment, the present disclosure further comprises combusting off gas products and using the energy for drying heat exchange. In an embodiment, the present disclosure further comprises combusting off gas products and using the energy to produce electricity. In an embodiment, the present disclosure further comprises combusting off gas products and using the energy to produce mechanical energy. In an embodiment, the present disclosure further comprises combusting off gas products and using the energy to produce heat. In an embodiment, the present disclosure further comprises concentrating equipment (centrifuges, belt presses and similar concentrating equipment) for concentrating or isolating the biomass within or from a biomass resource. In an embodiment, the present disclosure further comprises sending algae laden water to a concentrating or drying unit directly driven or heated by geothermal for separating algae from water.

In an embodiment, the present disclosure further comprises geothermal production, injection or re-injection wells from which energy can be used. In an embodiment, the present disclosure further comprises an expander to convert geothermal heat energy to mechanical energy. In an embodiment, the expander is a turbine. In an embodiment, the expander is a piston.

In an embodiment, the expander is a screw. In an embodiment, the present disclosure uses mechanical energy from an expander to directly drive equipment relating to the concentrating or isolation of biomass, water and oil. In an embodiment, the present disclosure further comprises sending a portion of the effluent products of the second tube to feed a biomass.

In an embodiment, the biomass is algae. In an embodiment, a portion of the effluent products comprise carbon dioxide. In an embodiment, a portion of the products as used as feedstock for distillation process. In an embodiment, a portion of the products as used as feedstock for pyrolysis process.

In an embodiment, the present disclosure further comprises spalling the rock.

The present disclosure includes post processing of bio-oil/crude oil leaving it to be separated into light, distillate and heavy fractions prior to shipment. Oil stabilization to be accomplished by using an underground geothermal density and ionic separation unit that uses geothermal heat to drive density separation and ionic separation by bridging geothermal with piezo-electric rods that generate a voltage drop across the separation fluid due to the temperature gradient inside of the underground separation column. Thus, the column uses geothermal energy for heat and for ionic separation processes. Using density separation alone is not ‘cost-effective’ due to time constraints (in yellow grease tanks, the separation goes slower during the winter and faster during summer)—however, ionic separation is also used to speed-up separation processes, which is typically driven by an applied electrical voltage. Ionic separation columns use voltage differential to separate polar/ionic mixtures. Reversible piezoelectric materials generate temperature differences when driven by an applied voltage. This reversible process can also be used to generate a voltage differential when element sides are exposed to a “Delta T” temperature difference.

In an embodiment, processing can include but is not limited to, use of liquid alkali, alkaline, transitional, other metals, water, brine and various other compounds as heat transfer fluid, desulfurization, demetalization, lowering total acid number and hydrogenation; Demineralization Unit (DMIN) to remove minerals for resale via cooling, heator magnetic b-fields (ancillary revenue stream); separation of process fluid in tubular reactor from geothermal reservoir fluid by use of a working heat transfer fluid. The intent is to reduce maintenance by restricting the geothermal fluid to the pipe inner diameter for pigging to minimize downtime; The use of a pipe cleaning object that dissolves into oil and gas (due to hydrothermal processes that depolymerize), such as a dissolving pig, when injected into the tubular reactor and never returns, but cleans the pipe I.D. and O.D.

Various embodiments of the disclosure include:

1. An underground reactor for use in creating fuel from organic material, comprising: a first conduit that injects an organic material underground; a second conduit that collects reacted organic material produced by the underground reactor; a heat exchanger for extracting heat; a biomass source; and concentrating equipment that separates the biomass from its cultivation medium.

2. The underground reactor of Claim 1, further comprising a plurality of capillary injection tubes.

3. The underground reactor of Claim 1, wherein the heat exchanger is used for powering equipment used in the creation process of a substance selected from the group consisting of oil and fuel.

4. The underground reactor of Claim 1, wherein the concentrating equipment is a centrifuge.

5. The underground reactor of Claim 1, further comprising an expander powered by geothermal energy.

6. The underground reactor of Claim 5, wherein the expander is a turbine.

7. The underground reactor of Claim 5, wherein the expander powers the concentrating equipment.

8. The underground reactor of Claim 1, wherein the biomass source is a biomass farm that grows the organic material.

9. An underground reactor for use in creating hydrocarbons from organic material, comprising: a first conduit that injects an organic material underground; a second conduit that collects reacted organic material produced by the underground reactor; and a heat exchanger for extracting heat; wherein the organic material is pulverized coal.

10. The underground reactor Claim 9, further comprising a plurality of capillary injection tubes.

11. The method of Claim 9, wherein the heat exchanger is used for powering equipment used in the fuel creation process.

12. A method of performing a high-pressure, high-temperature reaction comprising:

sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals;

bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit;

using a heat exchanger for extracting heat; and

sending geothermal fluid to a biomass growth.

13. The method of Claim 12, wherein the geothermal fluid comprises carbonates and biocarbonates.

14. The method of Claim 12 further comprising injecting super-critical fluid through capillary tubes in the first conduit.

15. The method of Claim 12, wherein the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, or chemicals.

16. The method of Claim 12, further comprising adjusting pressure by a method selected from the group consisting of increasing tubular reactor depth, decreasing tubular reactor depth, increasing back pressure at surface, decreasing back pressure at surface, and loading the tubular reactor working fluid with high specific gravity material mixed within the working fluid.

17. A method of performing a high-pressure, high-temperature reaction comprising:

sending biomass underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals;

bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit;

using a heat exchanger for extracting heat; and

circulating fluid in a closed loop to keep the biomass growth at a desired temperature.

18. The method of Claim 17 further comprising injecting super-critical fluid through capillary tubes in the first conduit.

19. The method of Claim 17, wherein the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, or chemicals.

20. A method of performing a high-pressure, high-temperature reaction comprising:

separating biomass from its cultivation medium;

sending the biomass underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals;

bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit; and

using a heat exchanger for extracting heat.

21. The method of Claim 20 further comprising injecting super-critical fluid through capillary tubes in the first conduit.

22. The method of Claim 20, wherein the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals.

23. The method of Claim 20, wherein the cultivation medium is water.

24. The method of Claim 23, further comprising skimming equipment for dewatering.

25. The method of Claim 23, wherein the water is separated from the biomass using geothermal heat.

26. The method of Claim 20, wherein the biomass is separated from its cultivation medium using concentrating equipment.

27. The method of Claim 26, wherein the concentrating equipment is at least one centrifuge.

28. The method of Claim 26, further comprising using geothermal energy to power the concentrating equipment.

29. The method of Claim 28, wherein the geothermal energy is harnessed through at least one expander.

30. The method of Claim 29, wherein the expander is a turbine.

31. The method of Claim 20 further comprising adjusting the reactor temperature by a method selected from the group consisting of increasing pump-around flow rate, decreasing pump-around flow rate, increasing tubular reactor flow rate, decreasing tubular reactor flow rate, increasing tubular reactor inlet temperature, decreasing tubular reactor inlet temperature, increasing pump-around re-injection temperature, increasing super critical fluid flow rate, decreasing super critical fluid flow rate, increasing super critical fluid temperature, decreasing super critical fluid temperature, changing the super critical fluid composition, increasing super critical fluid pressure, decreasing super critical fluid pressure, or increasing or decreasing back pressure at surface or loading the tubular reactor working fluid with high specific gravity material mixed within the working fluid, independently adjusting super critical fluid pressure, temperature, flow and composition within each injection tube or capillary, and decreasing pump-around re-injection temperature.

Some helpful features of the disclosure include: a) Pig Friendly Design for easy scale removal on heat transfer fluid side in contact with formation fluids (geothermal reservoir) (a key difference between pig friendly design and prior design is the heat transfer fluid flowing within the inner diameter (I.D.) of the pipes. Pigs work best when they're servicing the I.D. of a pipe and not the O.D.); b) Demineralization Unit (DMIN) to remove minerals for resale via cooling or magnetic b-fields (ancillary revenue stream); c) Fins on heat transfer pipe transfer heat into working fluid contained within casing and act as baffles to break vortexes generated from mixer system, which forces convective heat transfer to the tubular reactor (Fins can also be on tubular reactor.); d) Mixer/paddles/screws that mix casing working fluid to create convective heat transfer to tubular reactor; e) Gear box that drives the downhole mixer—to be powered by ORC unit; f) Geothermal reservoir fluid isolation from pipe O.D. —scale can be pigged from I.D. with minimal downtime as this configuration does not require tubular removal (no tripping and downhole service downtime for weeks if not months); g) Convective heat transfer using rotational speed of mixer(s); and h) Bio-oil stabilization: Downstream bio-oil processing will occur in a topping unit, to separate out light ends, distillate and heavier 6 oil material with later downstream oxygenate and nutrient recovery processing steps prior to leaving facility gates for refinery or petrochemical delivery. By incorporating a small topping unit and nutrient recovery into The underground subsurface reactor's infrastructure, select cuts of hydrocarbon can be specifically tailored to fluidized catalytic crackers (FCC) or (“cat-crackers”) and delayed coking units for a given refiner or petro-chemical complex to optimize finished product ASTM specs, while maximizing valuable nutrient recovery at the underground subsurface reactor facility. The key difference in the underground subsurface reactor's topping unit is that it de-couples fossil fuel use to separate fossil fuel into select fractions of light ends, distillate and heavy 6 oil bottoms. The underground subsurface reactor accomplishes the oil fractionation using geothermal ionic separation technology, which uses geothermal derived loop heat pipe to drive density separation with latent heat capillary flow and piezoelectric material to create a voltage in response to the geothermal temperature gradient and stress from hydraulic head. Thus, liquid phase separation occurs underground due to temperature, capillary action, stress and voltage gradients created and sustained by geothermal heat, wicking material selection, piezoelectric material selection and gravity.

In some instances the geothermal heat and associated gradient is not sufficient to meet reactor conditions due to reduced permeability associated with scale and plugging over the lifetime of operating the underground reactor system. Additionally, it can be required to run the tubular reactor at higher temperatures. Thus, pre-heating the inlet to the tubular reactor and working heat transfer fluid through either combustion (recycling the effluent CO2 to the algal pond), electric heater or concentrating solar power (CSP) can prove to be an effective solution in delaying re-fracking and stimulation of the reservoir. Additionally, super critical fluid injection through capillary tubes will assist in downhole reaction and temperature control.

Advantages of embodiments of the present disclosure include: use of a cleaning/pigging device to remove scale/fouling; use of a working heat exchange fluid to isolate the geothermal reservoir fluid from fouling the tubular reactor; use of underground agitator(s) to force convective heat transfer; use of underground piezoelectric/thermal particles to transform stress into heat; use of underground catalyst; and use of underground vapor collapse to generate latent heat.

BRIEF DESCRIPTION OF THE DRAWINGS

In order that the manner in which the above-recited and other enhancements and objects of the disclosure are obtained, a more particular description of the disclosure briefly described above will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. Understanding that these drawings depict only typical embodiments of the disclosure and are therefore not to be considered limiting of its scope, the disclosure will be described with additional specificity and detail through the use of the accompanying drawings in which:

FIG. 1. Reactor well head with super-critical fluid capillary injector manifold, catalyst injector, solvent injector, product recovery, heat transfer fluid injector, heat transfer fluid recovery, cellar, and downhole casing.

FIG. 2A. Super-critical fluid injectors downhole within the tubular reactor.

FIG. 2B. Super-critical fluid injectors downhole within the tubular reactor.

FIG. 2C. Super-critical fluid injectors downhole within the tubular reactor.

FIG. 2D. Super-critical fluid injectors downhole within the tubular reactor.

FIG. 3. Process flow diagram of the underground reactor system with preheating of feedstock, super-critical fluid, solvent, and catalyst.

FIG. 4. Perspective drawing from downhole looking up to the surface in a tubular reactor.

FIG. 5. An exemplary geothermal depolymerization tubular reactor.

FIG. 6. An exemplary underground reactor system.

FIG. 7. Exemplary underground reactor fluid flow.

FIG. 8. Exemplary hydro-geothermal reactor process flow diagram.

FIG. 9. Exemplary hydro-geothermal reactor process flow diagram.

FIG. 10. An exemplary geothermal tubular reactor.

FIG. 11. An exemplary geothermal tubular reactor.

FIG. 12. An exemplary geothermal tubular reactor.

FIG. 13. An exemplary geothermal tubular reactor.

FIG. 14. An exemplary geothermal tubular reactor.

FIG. 15. An exemplary geothermal tubular reactor where there is no pump-around tube, the inlets and outlets are separated and there is no casing.

FIG. 16. Working heat transfer temperature curve inside of casing.

FIG. 17. Working heat transfer temperature profile inside of casing subjected to forced convection.

FIG. 18. Tubular reactor profile.

FIG. 19. Tubular reactor profile subjected to forced convection.

FIG. 20. Illustration of isolated hot geothermal reservoir fluid from hot working fluid from reactor process fluid.

FIG. 21. Tubular reactor with geothermal reservoir fluid casing injection.

FIG. 22. Tubular reactor with external geothermal reservoir fluid injection.

FIG. 23. Tubular reactor with isolated geothermal reservoir fluid.

FIG. 24. Tubular reactor with isolated geothermal reservoir fluid and forced convection.

FIG. 25. Tubular reactor using piezothermal/electric particles and catalyst.

FIG. 26. Tubular reactor using gas injection isolated from geothermal reservoir fluid.

FIG. 27. Computational fluid dynamics (CFD) model of casing, tubular reactors and hot geothermal transfer pipes.

FIG. 28. An exemplary schematic of a turbine and geothermal centrifuges incorporated into the system.

Calculations. The sheets attached after the figures in U.S. Provisional Patent Application Ser. No. 61/602,841 provide calculations illustrating the feasibility of embodiments of the present disclosure.

DETAILED DESCRIPTION

The particulars shown herein are by way of example and for purposes of illustrative discussion of the preferred embodiments of the present disclosure only and are presented in the cause of providing what is believed to be the most useful and readily understood description of the principles and conceptual aspects of various embodiments of the disclosure. In this regard, no attempt is made to show structural details of the disclosure in more detail than is necessary for the fundamental understanding of the disclosure, the description taken with the drawings making apparent to those skilled in the art how the several forms of the disclosure can be embodied in practice. The following definitions and explanations are meant and intended to be controlling in any future construction unless clearly and unambiguously modified in the following examples or when application of the meaning renders any construction meaningless or essentially meaningless. In cases where the construction of the term would render it meaningless or essentially meaningless, the definition should be taken from Webster's Dictionary 3rd Edition.

As used herein the term, “conduit” means and refers to a pipe, tube, tubular, duct, trough, or channel.

As used herein the term, “capillary injection” means and refers to use of capillary tubing for adding a substance to a given location.

As used herein the term, “downhole” means and refers to inside the well itself.

As used herein the term, “geothermal” means and refers to generation and storage in the earth.

As used herein the term, “raceway” means and refers to a shallow pond for the cultivation of algae.

As used herein the term, “off-gas” means and refers to a flammable gas produced as the result of a process. Off-gas can include but is not limited to a mixture of methane, ethane, ethylene, propane, propylene, and butane.

As used herein the term, “light ends” means and refers to components of a mixture of hydrocarbons that boil at lower temperatures than the bulk of the mixture. Light ends can be distilled at atmospheric pressure. Light ends can include but is not limited to butane and light components of the mixture.

As used herein the term, “heavy ends” means and refers to components of a mixture of hydrocarbons that boil at higher temperatures. Heavy ends can include but are not limited to high molecular weight alkanes, alkenes, and high molecular weight aromatic compounds.

As used herein the term, “pig” means and refers to a structure that fits within a pipe to clean, test, or block the pipe.

Dedicated geothermal tubular reactor (Hydrolysis, Depolymerization, Decarboxylation, and Thermal Degradation). Downhole temperatures and pressures exist to create and sustain hydro-geothermal reactions and thermal depolymerization given available geothermal energy within the earth. Bedrock temperature as a function of depth will be used as the reference temperature driving force. The tubular depolymerization reactor section will be modeled with the casing full of water that is not subject to forced circulation.

Hydro-Geothermal Reactor

TABLE 1 Depolymerization variables of interest VARIABLE DESCRIPTION T_(inlet) Reactor inlet temperature T_(outlet) Reactor outlet temperature T_(i, rock) Rock temperature profile T_(i, down) Downward flowing fluid temperature T_(i, up) Upward flowing fluid temperature R_(f) Algae to Water Ratio F_(inlet) Algae flow rate at reactor inlet t_(oil) Total algae residence time F_(casing) Water flow rate in casing

FIG. 1 depicts a tubular reactor with super-critical fluid injection tubes for capillary injection. The tubular reactor can include a well head 102, cellar 104, and downhole casing 108. The well head can include but is not limited to top valve(s), pack-off assemblies, capillary super critical fluid tubing manifold, capillary tubing, downhole instrumentation, and service valves. The cellar can include but is not limited to a casing spool, casing head, and master valve(s). The downhole casing can enclose a tubular reactor, capillary super-critical solvent injection and heat transfer pump. The well head includes but is not limited to an injection capillary 114, tubular reactor return 115, top valves 116, super-critical fluid capillary injector manifold 117, super-critical fluid capillaries 118, and tubular reactor injectors 119. The cellar includes but is not limited to a heat transfer pump injector and return 110 and master valves 111.

FIGS. 2A-2D depict super-critical fluid injectors downhole within the tubular reactor. At the surface, a fluid is heated up under pressure to provide a super-critical fluid (high temperature & pressure). The super-critical fluid is injected through the tubulars or capillary tubes to in-situ hydrogenate, hydrolyze, and crack the heavy oil hydrocarbon in the tubular reactor into lighter components via a direct liquefaction reaction. The super-critical fluid injected downhole does not cool down because the heavy oil or other material in the tubular reactor will be sub-critical. Insulation can be present around the tubular or capillary injectors in the form of ceramic, kaowool, gas, or other insulating material. The tubing flow channel 202 for super critical fluid (SCF) for 1) downhole flow into a tubular reactor or 2) to house and insulate capillary tubing of 2″ or less for SCF injection. Minimizing the cooling of the SCF fluid in order to prevent the SCF fluid temperature from lowering and going sub-critical, which adversely impacts downhole reaction. The tubing wall 204 encloses the flow channel to house capillary tubing or insulation material, such as Kaowool, ceramic filler, or SCF. The tubular reactor return pipe 206 or coiled tubing wall separates the feedstock input traveling downhole in downflow region 216 from the in-situ reaction and reaction products upflowing through upflow region 212. Sheath 208 contains the tubing flow channels and capillaries listed in 202 and 204 and insulates the SCF flowing downhole from cooling effects. The inner set of tubular flow channels 210. The channels have the option to be connected to flow channels 202, 204 or independent. The upflow region 212 is used for in-situ reaction, reaction products, and unreacted feedstock to be recycled. The void space 214 between tubing flow channels can be used for insulation or instrumentation and electronics housing. The downflow region 216 where feedstock flows downhole inside of the tubular reactor and then upflows after hitting the tubular reactor's bottom hole cap at 226. The down flow is contained by tubular reactor wall 218 with cap 222 and 226. The tubular reactor outer wall 218 resides within the casing and can be immersed in heat transfer fluid. Select tubing flow channels 220 and capillary tubing can extend beyond the depth at which return wall 206 stops. The tubular reactor's closed-loop downhole system can include a cap 222. A super critical fluid (SCF) 224, solvent, catalyst, or chemical combination can be injected through the tubular reactor and/or capillary tubing. The tubular reactor's closed-loop downhole system can include a bottom hole cap 226.

FIG. 3 depicts a process flow diagram of the underground reactor system with preheating of feedstock, super-critical fluid, solvent, and catalyst. In Item 3.1, Feedstock 302 comprised carbon-based organic material, for example wet or dry micro-algae, macro-algae, lignin, lignocellulosic, bitumen, lipids, cellulose, etc; Carbon Dioxide can be recycled to cultivate and boost productivity. In Item 3.2, Super critical fluid (SCF) 304 can be comprised of including but not limited to water, hydrogen, alcohol, an organic such as carbon-dioxide, methane, ethane. In Item 3.3, Catalyst 306 can be comprised of pyrite, sulfur, iron, cobalt, sodium, salts, metals, carboxylic acids, rare earths, etc. In Item 3.4, Heat exchanger 308 preheats feedstock, the feedstock 302 (Item 3.1) can bypass based upon operational mode and heat demands. Additionally, if required feedstock can be ran through heater 312 (Item 3.6). In Item 3.5, Heat exchanger 310 preheats, SCF (Item 3.2), the SCF 304 can bypass based upon operational mode and heat demands. Additionally, if required SCF 304 can be ran through heater (Item 3.6). In Item 3.6, Heater 312 is used to heat solvent and/or feedstock and/or catalyst, can be natural gas fired heater, solar furnace, geothermal, nuclear, coal, lignite, bitumen, coke, electrical, induction, resistive, etc. and use natural, radiant, and convective heat transfer. In Item 3.7, Underground Reactor 314 is used to convert feedstock 302 (Item 3.1) in combination with SCF 304 (Item 3.2), hydrogen transfer solvent (Item 3.8) catalyst 306 (Item 3.3), and carbon-monoxide) into liquid oil and gas hydrocarbons. In Item 3.8, Solvent Regenerator 316 receives recovered spent hydrogen transfer solvent, for example tetraline, from (Item 3.9) separator 318 or refinery off-gas, or refinery acid-gas, or indirect liquefaction reaction from coke or other carbon feedstock to hydrogenate the dehydrogenated solvent with hydrogen, methane and/or di-hydrogen sulfide before injection into underground reactor 314 (Item 3.7). In Item 3.9, Separator 318 receives the underground reactor effluent (Item 3.7) and separates out liquid hydrocarbons, solvent, gas (condensable and non-condensable), solids and unconverted feedstock for downstream processing or recycle. In Item 3.10, Liquid oil product 320 includes but is not limited to hydrocarbon, synthetic crude oil with API 0 . . . 70. In Item 3.11, Turbine 322 is a direct drive to pumps for reactor system to move feedstock, SCF, solvent, catalyst and product and can also be used to generate electricity with generator. In Item 3.12, the Refinery or Plant 324 receives converted hydrocarbon oil product and produces fuels, chemicals and other salable products from the source hydrocarbon and balance of plant processes.

FIG. 4 depicts a perspective from downhole looking up to the surface in a tubular reactor. Capillary tubes 402 are present in a circle within the tubular reactor 418.

The algae laden water from an above ground raceway, open pond or settling tank system is injected downhole into the closed loop hydro-geothermal reactor. Algae species that can be utilized in the present disclosure include but are not limited to Botryococcus braunii, Chlorella, Dunaliellla tertioleccta, Gracilaria, Pleurochrysis carterae, Sargassum, Ankistrodesmus, Chlorella, Cyclotella, Hantzschia, Nannochloris, Nannochloropsis, Nitzschia, Phaeodactylum tricornutum, Scenedesmus, Stichococcus, Tetraselmis suecica, Thalassiosira pseudonana, Crypthecodinium cohnii, Neochloris oleoabundans, and Schiochytrium. When the downhole algae in water pressure and temperature exceeds atmospheric and ambient temperature the algae and other organic matter undergoes hydrolysis and partial thermal degradation to form carbon, CO₂, off-gas, hydrocarbon and hot mineral rich water containing amino acids. The tubular reactor is primarily located inside of the casing, but can extend outside of the casing into an open end region. The casing contains hot water that is either static or being circulated through a pump-around system either under natural hydraulic head or subject to geo-pressure from the rock formation, while being counter-balanced with above ground force. An exemplary embodiment is shown in FIG. 5.

Algae laden water 114 is injected at the surface downhole through the annular space and flows deep underground. The algae laden water flows downhole where the geothermal temperature and hydrostatic head of the water column provide the conditions required for the geothermal depolymerization reaction to occur. The sterilized and hot water converts algae into synthetic crude oil then flows back up to the surface after safely hydrolyzing/depolymerizing miles underground. An underground geothermal reservoir is present at the bottom of the downhole.

In one embodiment, separate geothermal production wells can be drilled where the energy from those wells can operate concentrating equipment, such as centrifuges, to separate algae laden water into algae and water or separate water from oil in the reactor's product. The algae can then be pumped into the reactor. In some embodiments, the geothermal production wells can be connected to an expander that will convert the geothermal heat energy directly into mechanical energy to operate the centrifuges. In an embodiment, the expander is a turbine. This will reduce parasitic energy losses as converting geothermal heat energy to mechanical work to drive an expander to generate electricity and then conversion and transmission of electricity over power lines only to be converted back into mechanical energy is less efficient than direct driving process and concentrating equipment. In a preferred embodiment, geothermal systems (steam, single flash, double flash, single flash with binary bottoming unit, single flash with kalina bottoming cycle, binary plant, or kalina plant) will serve the motive force (direct drive) needs of the processing and concentrating equipment, such as belt presses and centrifuges.

In one embodiment, the tubular reactor can be curved at deeper depths to allow for the biomass to access greater hot geothermal rock for increased surface area.

The geothermal source can be either geo-pressured or not.

In some embodiments, the depth of an underground reactor can range from 33 ft-40,502 ft (10 m-12,345 m). FIG. 11. In some embodiments, a tubular reactor outer pipe can have a diameter of 1 inch to 100 ft (25 mm to 30 m), a tubular reactor inner pipe can have a diameter of 1 inch to 100 ft (25 mm to 30 m), and a casing can have a diameter of 1 inch to 100 ft (25 mm to 30 m). FIG. 10. Certain embodiments can have a curved or sloped tube in order to have a longer period of time in the reactor. A sloped tube can have a series of slopes gradually turning more horizontal as it moves deeper. As dry oil and gas exploration, production and geothermal holes can be used in the present disclosure, the tubing used in such installations will be sized appropriately to fit therein. For example, in a hole of about 5,000+ feet (1,524+m) in length, the tubing diameters will likely be about 12 up to 120 inches (30-305 cm).

In some embodiments, there can be more than one tubular reactor.

In some embodiments, temperatures needed for an effective reaction can be greater than 100° C. and up to 2,000° C., and pressures needed for an effective reaction can be 14.7 psig (203 kPa) up to 40,000 psig (275,892 kPa).

Based on the temperature and pressure ranges within the reactor, liquefaction thermochemical or hydrothermal processes can occur within the reactor during certain ranges of T and P in water:

-   -   100° C. up to 374° C. (subcritical water) and 14.7 psig (203         kPa) up to 30,000 psig (206,944 kPa)     -   374° C. up to 500+° C. (supercritical water) and 14.7 psig (203         kPa) up to 30,000 psig (206,944 kPa)         Some embodiments can use any type of organic matter to create         products within the reactor under the relevant temperature and         pressure conditions. In certain embodiments, polymers can be         used as an organic matter for reaction within a solvent (for         example: water) in an underground reactor. An exemplary         underground reactor system is depicted in FIG. 6.

As depicted in FIG. 13, the tubular reactor inside pipe diameter can be equal to or greater than 1 inch and less than or equal to 100 feet. The tubular reactor outside pipe Diameter can be equal to or greater than 1 inch and less than or equal to 100 feet. The pump-around tubular Diameter can be greater than 1 inch and less than 100 feet. Flow direction can be either downhole or reversed. The casing Diameter can be equal to or greater than 1 inch and less than or equal to 100 feet. The casing can also “neck down” into smaller diameter casings depending upon depth. The pump-around tubular can extend past the tubular reactor and both the tubular reactor and pump-around tubular can extend past the casing and into the frac'd rock.

As depicted in FIG. 11, the pump-around tubular 1108 can be open-ended at bottom and can also contain open areas for fluid to flow through other than the bottom. The underground reactor depth can be as shallow as 33 feet or as deep as 40,502 feet. The underground reactor pressures up to 40,000 psig. The underground reactor temperatures range from 200 degrees F. to 4,000 degrees F. The tubular reactor inner pipe 1106 can have an open end to facilitate flow through the annular space inside of the tubular reactor, which is isolated from the casing and pump-around flow. The tubular reactor can have a closed end outer pipe.

As depicted in FIG. 12, the tubular reactor inner pipe 1206 can have an open end to facilitate flow through annular space inside of the tubular reactor, which is isolated from the casing and pump-around flow. The tubular reactor outer pipe 1204 can have a closed end to facilitate flow through annular space inside of the tubular reactor, which is isolated from the casing and pump-around flow. The pump-around tubular 1208 can be open-ended at the bottom and can also contain open areas for fluid to flow through other than at the bottom.

As depicted in FIG. 13, the tubular reactor inside pipe 1306 diameter can be equal to or greater than 1 inch and less than or equal to 100 feet. The pump can be downhole or at the surface. There can be coiled tubing or pipe for the inner pipe. The tubular reactor outer pipe 1304 diameter can be equal to or greater than 1 inch and less than or equal to 100 feet. There can be coiled tubing or pipe for the outer pipe. The casing 1310 diameter can be equal to or greater than 1 inch and less than or equal to 100 feet. The casing 1310 can also neck down into smaller diameter casings depending upon depth. The tubular reactor inner pipe 1306 can have an open end to facilitate flow through annular space inside of the tubular reactor, which is isolated from the casing and pump-around flow. The pump-around tubular 1308 is open-ended at the bottom and can also contain open areas for fluid to flow through other than the bottom. The pump-around hot return flow passes up through the annular space between the pump-around tubular(s) or coiled tubing(s) and the tubular reactor(s). The flow can be reversed as well so that it flows down the annular space 1312 and up the pump-around tubular 1308. The pump-around tubular 1308 diameter can be greater than 1 inch and less than 100 feet. Flow direction can be either downhole or reversed.

As depicted in FIG. 14, the pump-around tubular 1408 diameter can be greater than 1 inch and less than 100 feet. Flow direction can be either downhole or reversed. The hot effluent routes to an Organic Rankine Cycle (ORC) binary geothermal power plant with a direct drive pump option to power pump-around(s) and/or tubular reactor(s) injection pumps. Hot water or thermal fluid can be used in the drying processes. The pump-around annular space hot effluent can flow to an Organic Rankine Cycle (ORC) binary geothermal power plant with direct drive pump option to power the underground reactor pumps. It can be used in drying processes and feature a back-pressure controller.

As depicted in FIG. 15, biomass is injected downhole with water and/or a catalyst including but not limited to sulfuric acid, pyrite, sulfur, iron, cobalt, sodium, salts, carboxylic acids, or rare earths. The injection casing/pipe 1504 can have open ends on the top and bottom. The injection casing/pipe can have a diameter of 1 inch to 100 feet. There can be more than one injection casing(s)/pipe(s) with additional take-offs. The temperature underground can be greater than 200 degrees F., with a pressure of greater than 14.7 psig, and a depth greater than 33 feet. After frac'ing the rock is porous and permeable. The rock surrounding the frac'ing region is non-porous and non-permeable. The injected biomass flow through the frac'd region and into the return casing/pipe for hydrocarbon recovery. The return casing/pipe can have a diameter of 1 inch up to 100 feet. The return casing/pipe contains liquefaction products including but not limited to hydrocarbon, gas, CO₂, and water. There can be more than one return casing(s)/pipe(s) with additional returns. The return products include but are not limited to crude oil, hot mineral rich water, CO₂, and off-gas that can be combusted. The return casing/pipe 1506 can have open ends on the top and bottom.

Some embodiments can use organic matter to produce chemicals, fuel or hydrocarbons depending on the organic matter used.

Some embodiments can use pulverized low to medium grade coal fed to the reactor which will undergo coal liquefaction. This reaction will result in carbon dioxide, off-gas, oil, tar and a remaining higher grade coal, such as bituminous or anthracite.

In some embodiments, there can be a dedicated geothermal tubular with multiple tubulars with a coiled tubing option for increased forced convection heat-transfer at one or multiple geothermal heat mines. Effluent geothermal fluid flow can exit into an organic rankine cycle (ORC). The organic rankine is comprised of a vaporizer/preheater that uses the heat from the effluent geothermal tubular pump-around fluid to heat and vaporize the working organic fluid. The working organic fluid (for example: n-butane) fluid vapors drive a turbine and the turbine exhaust vapors can be force-draft cooled with hot air for use in drying processes and later water cooled to provide additional warmth to algae ponds. The condensed working organic fluid can then be recycled back to the vaporizer for re-heating. The turbine can be connected to an injection pump and generator to produce electricity.

Embodiments with a tubular geothermal pump-around can provide tunable temperature control for the hydro-geothermal and depolymerization reactor by adjusting the pump around hot water flow rate and number of coiled tubing inserts. An exemplary embodiment of this feature is illustrated in FIG. 7. Some embodiments can use any heat transfer fluid to flow through the reactor and tune the temperature.

Geothermal fluid (water) 724 is pumped through the tubular pump-around 708 and discharged into the casing or rock depending upon flow direction. The geothermal fluid (water) is being pumped, inside of the tubular pump-around, to be discharged back inside of the casing 710. Pump suction or discharge pulls/pushes hot geothermal fluid (water) from/to bottom hole open-ended tubular at the hot geothermal rock/water interface. An underground geothermal reservoir is present at the bottom of the downhole.

In some embodiments, reactor temperature can be adjusted by increasing or decreasing pump-around flow rate, increasing or decreasing tubular reactor flow rate, increasing or decreasing tubular reactor inlet temperature or increasing or decreasing pump-around re-injection temperature.

TABLE 2 Geothermal pump-around key variables VARIABLE DESCRIPTION T_(inlet) Bottom hole inlet temperature T_(outlet) Discharge outlet temperature T_(i, rock) Rock temperature profile T_(i, down) Downward flowing fluid temperature in casing T_(i, up) Upward flowing fluid temperature in tubular F_(casing) Water flow rate in casing F_(inlet) Water flow rate in tubular t_(tube) Total water residence time in tubular t_(casing) Total water residence time in casing

If pump-around delivers enough heat via forced convection, then a shallower depth can be sufficient for the reactor in order to reach required temperatures. Without the tubular pump-around, greater drilling depths for a given geothermal resource would be required due to heat transfer limitations in the tubular pump-around, casing and downhole open-end region.

In some embodiments, a pump-around pipe can have a diameter of 1 inch to 100 ft (25 mm to 30 m).

Some embodiments can use a heat exchanger to extract energy from the heated heat transfer fluid. Examples of heat exchange devices that can be used include Rankine, Carnot, Stirling, Heat Regenerative Cyclone, thermoelectric (peltier-seebeck effect), Mesoscopic, Barton, Stoddard, Scuderi, Bell Coleman and Brayton. In yet other embodiments, off-gas products can be combusted to heat a heat transfer fluid for use in a heat exchanger. The heat transfer fluid can be used for drying, producing electricity, heating aspects of the reactor, or producing mechanical energy.

Yet other embodiments can use an organic rankine cycle to directly drive a pump to feed the heat transfer fluid into the geothermal pump-around system, power a downhole pump in the tubular reactor and produce electricity. Further, the condensing section of the organic rankine cycle can be used to assist in drying algae biomass or other organic materials when combined with a forced draft system powered by electricity or direct drive. Further, the organic working fluid in the condensing section can serve to warm algae ponds.

Hot Effluent Water Containing Minerals, Amino Acids and Carbon

The tubular reactor's effluent products can contain sterilized mineral rich water, carbon and a hydrocarbon/gas mixture. The processes of depolymerization, hydrolysis, decarboxylation, and thermal degradation result in the formation of a hydrocarbon oil/gas/carbon/carbon-dioxide mixture. The solid carbon and hydrocarbon is formed by a combination of depolymerization, hydrolysis, decarboxylation, and thermal degradation underground. Some embodiments can include standard oil/water/gas separation equipment to separate the hydrocarbon and gas.

Post-separation, the oil-free hot tubular reactor's mineral rich effluent water can be returned back to the open algae farm raceway system or other biomass system. In some embodiments, total hot water return volume can be set at ⅓ of raceway water volume, so that ⅓ of the raceway water can be turned over and processed each day.

In some embodiments, the separated gas mixture and carbon dioxide can be combusted to generate electricity, heat and carbon dioxide. The carbon dioxide can be injected downhole into the tubular reactor's effluent to assist in pumping as well as into the effluent stream prior or after being recycled back into algae pond or break tank.

In some embodiments, the reactor's maximum size is a function of the hydro-geothermal depolymerization reactor's effluent flow rate, temperature, mineral content, amino acid content and carbonation, which is dependent upon the geothermal resource, tubular reactor depth, pump-around rate and direction.

Environmental variables that impact the reactor can include ambient temperature, wind velocity, cloud cover, evaporation rate, precipitation, relative humidity, and atmospheric pressure. Key process variables include reactor effluent flow rate and temperature in addition to the algae pond dimensions such as depth, width, length, and circulation.

TABLE 3 Algae Raceway & Process Variables VARIABLE DESCRIPTION T_(outlet) Reactor outlet temperature F_(outlet) Reactor outlet flow rate T_(amb) Ambient temperature v_(w, xy) Wind velocity and direction F_(discharge) Pond discharge rate E_(rate) Evaporation rate P Precipitation R_(H) Relative humidity P_(atm) Atmospheric pressure P_(depth) Algae pond depth P_(length) Algae pond length P_(width) Algae pond width T_(x, y, z pond) Algae pond temperature distribution F_(x, y, z) Algae pond circulation Production of Carbon Dioxide Underground from Algae in Water, Biomass, Waste and Polymers

Carbon dioxide can be produced during the decarboxylation step in the presence of water, heat, pressure, algae, biomass, waste, and polymers underground in the tubular. In some embodiments, the carbon dioxide can be recycled within the process.

Production of Hydrocarbon Liquid/Gas Mixture Underground from Algae in Water, Biomass, Waste and Polymer Created from Geothermal Driven Hydrolysis and Thermal Degradation

When the algae in water, biomass, waste water, waste and polymer are subject to pressures and temperatures above ambient (300+° F. (149+° C.) and 300+ psig (2,170+ kPA)) underground the material undergoes hydrolysis, decarboxylation and degradation to form the oil and gas along with solid carbon, carbon dioxide and hot mineral rich water. In some embodiments, the oil/gas/water mixture is then separated with the water recycled to the algae pond and the oil and gas sent to downstream processing units for electricity, heat, chemical, transport fuel, and coke production. Exemplary flow charts indicating this process is illustrated in FIGS. 8 and 9. Coke production can occur via pyrolysis.

TABLE 4 Hydro-Geothermal Reactor Streams STREAM DESCRIPTION F1 Algae in water 814 raceway is injected into Hydro- Geothermal Reactor 826 P1 Produced oil from reactor 828 P2 Produced light end gas 832 and CO₂ 830 P3 Produced mineral 834 and amino acid 836 hot effluent water to be recycled back into algae pond for N—P—K and Temperature algae growth multiplicative enhancement

Benefits for existing industrial facilities & algae cultivation include renewable oil production, industrial waste water consumption and multiplicative growth enhancement for large scale algae farm with CO₂ and mineral rich hot water.

In addition to recycling the CO₂ and warm mineral rich water back to the algae farm to assist with growth, the fluid, containing CO₂, from underground (“geothermal fluid”) can be pumped into the algae farm to assist with algal productivity as well. When the geothermal fluid's temperature increases or pressure decreases, CO₂ evolves from the liquid phase into the gas phase. Thus, extracting CO₂ from geothermal fluid or process fluid can be accomplished by flashing the CO₂ in a flash vessel, tank or cyclone separator at the production well or geothermal facility prior to re-injection of the geothermal fluid into the reservoir or algae cultivation system. Further, silica, silicates, phosphorous, potassium, iron, cobalt, copper, gold, potassium, chromium, vanadium, selenium, molybdenum, sulfur, chlorine, boron, sodium, zinc, Manganese, nitrogen, and iodine, present in geothermal fluid water can be recycled to the algae farm to boost algae (for example: diatom) productivity levels.

Additionally, a working fluid, such as ethylene glycol or propylene glycol can be circulated in a closed-loop system below the algae cultivation system to serve as cooling. The difference between this fluid loop (closed or open) and the geothermal fluid is that at shallow depths the earth is at near constant temperatures 30-100 degF. Thus, algal cultivation systems can be heated or cooled by heat transfer with geothermal fluids at different depths and temperatures.

Dehydration of algae can also be accomplished by exposing the wet algae to geothermal heat.

TABLE 5 The underground subsurface reactor process flow diagram (PFD) STREAM DESCRIPTION F0 Algae in aqueous phase 914 is fed into hydro- geothermal reactor 926 F1 Industrial waste water 938 is fed into hydro- geothermal reactor 926 F2 Combined waste water 938 and algae feed stream 914 to reactor 926 P1 Oil 928 produced from reactor 926 is then fed to coker 942 for gasification P2 Reactor light ends 932 and CO₂ 930 fed to turbine 940 P3 Hot water effluent enriched with minerals 934 and amino acids 936 recycled to algae pond to enhance growth rate C1 Coker light ends 952 and CO₂ 554 fed to turbine 540 for electricity 946, heat 950 and CO₂ 956 generation C2 Produced coke 944 can be used to generate electricity 946, heat 950 and CO₂ 956 TF Produced transportation fuel 948 can be processed into renewable gasoline, jet, kerosene and diesel. E Electricity 946 to power pumps and auxiliary equipment H1 Products of coke combustion include heat 990 and possibly low pressure steam if combined cycle gas turbine (CCGT) used T1 Combustion product of turbine 940 generates heat 950 and possibly low pressure steam if CCGT is used T2 Combustion product of turbine 940 generates CO₂ 956 and H₂O 938 H2 Combustion product of coke 944 generates CO₂ 956 and H₂O 938

FIG. 16 plots the bulk temperature profile of the closed-loop working heat transfer fluid inside of the casing. Heat transfer occurs through conduction, natural convection and radiant heat transfer. The working heat transfer fluid in the casing 2303 is plotted in FIG. 16. The working heat transfer fluid transfers heat from the geothermal reservoir fluid into the tubular reactor.

FIG. 17 plots the bulk temperature profile of the closed-loop working heat transfer fluid inside of the casing. Heat transfer occurs through conduction, natural convection and radiant heat transfer. The working heat transfer fluid in the casing 2003 is plotted in FIG. 17. The working heat transfer fluid transfers heat from the geothermal reservoir fluid into the tubular reactor.

FIG. 18 plots the tubular reactor temperature profile of the closed-loop process fluid inside of the reactor's annular flow space and center pipe return without forced convection. The tubular reactor (see 2319) is immersed in the working heat transfer fluid (see 2303). Process reactants enter the reactor (see 2315), also shown in the bottom left hand section of the plot. The process fluid flows underground through the annular space (see 2304) then returns through the center pipe (see 2305). The reactor temperature profile can be adjusted by adjusting the temperature and flow rate of injection stream 2314, demineralization flow rate 2313, organic rankine cycle flow rate 2316, concentration and distribution of piezo particles in the working heat transfer fluid (see 2621) or tubular reactor (see 2622), concentration and distribution of catalyst into the tubular reactor (see 2623), gas flow rate into the tubular reactor inlet line (see 2615), inlet temperature of process fluid 2315 and flow rate of process fluid 2315.

FIG. 19 plots the tubular reactor temperature profile of the closed-loop process fluid inside of the reactor's annular flow space and center pipe return with forced convection. The tubular reactor (see 2323) is immersed in the working heat transfer fluid (see 2303). Process reactants enter the reactor (see 2315), also shown in the bottom left hand section of the plot. The process fluid flows underground through the annular space (see 2304) then returns through the center pipe (see 2305). The reactor temperature profile can be adjusted by adjusting the temperature and flow rate of injection stream 2314, demineralization flow rate 2313, organic rankine cycle flow rate 2316, concentration and distribution of piezo particles in the working heat transfer fluid (see 2621) or tubular reactor (see 2622), concentration and distribution of catalyst into the tubular reactor (see 2623), gas flow rate into the tubular reactor inlet line (see 2615), inlet temperature of process fluid 2315, flow rate of process fluid 2315 and mixer rod rotational velocity 2618 b and mixer rod impeller, screw or paddle geometry 2618 b.

FIG. 20 lists the heat transfer mechanism and fluids used to confine geothermal reservoir fluid scaling, corrosion and depots to the inner diameter of the hot geothermal transfer pipe (see 2307). FIG. 16 depicts a heat transfer fluid system to minimize maintenance by containing geothermal reservoir fluid inside of the hot tubular, which transfers heat to the heat transfer fluid to process fluid. The geothermal reservoir fluid receives heat from the fracked hot rock and sedimentary geothermal resources 2002. The heater transfer fluid is isolated from the geothermal reservoir fluids and contained inside of the casing 2004. It is the heat transfer medium form the geothermal reservoir fluid to the tubular reactor process fluid. The tubular reactor process fluid flows underground through annular space in the tubular reactor, then flows back to the surface through the center pipe return 2006. The temperature is primarily driven by the heat transfer fluid. The purpose of isolating the hot geothermal reservoir fluids (injected or pre-existing) from the tubular reactor is to reduce maintenance downtime by providing pigging of the pipe inner diameter. Pigging is a process by which a plastic/rubber object with abrasive edges/cutters is driven by pressure through a pipe to typically clean the pipe's inner diameter from scale and other oxides/deposits that restrict heat transfer and fluid flow. If pigging was not able to be performed the entire tubular reactor would have to be removed to remove scale. Thus, by isolating the geothermal working fluid within a pipe and using a working heat transfer fluid (water, brine, mercury, etc.) to transfer heat from the isolated geothermal fluid into the tubular reactor, the feasible operation of an underground reactor is accomplished by significantly reducing maintenance downtime and costs.

FIG. 21 lists a casing contained injection and reactor configuration. The continuously stirred rods devices 2104 maintains high velocity flow rate along the outer diameter of the tubular reactor to minimize scaling and fouling by continuously sweeping the surface and aids in convective heat transfer. Geothermal reservoir fluid is injected in 2103 and flows downhole and into the reservoir 2109 and through the fracked rock 2110 and flows back out through the return pipe 2108 into the organic rankine unit 2102, which direct drives pumps and auxiliary equipment. The geothermal reservoir fluid directly contacts the outer diameter of the tubular reactor and can be drawn off through 2105 and 2102 streams for mineralization recovery through a demineralization unit (DMIN). The bottom hole temperature can exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).

FIG. 22 lists a casing contained reactor configuration with external injection line. The continuously stirred rods devices 2205 maintain high velocity flow rate along the outer diameter of the tubular reactor to minimize scaling and fouling by continuously sweeping the surface and aids in convective heat transfer. Geothermal reservoir fluid is injected in 2214 and flows downhole and into the reservoir 2210 and through the fracked rock 2209 and flows back out through the return pipe 2211 into the organic rankine unit 2216, which direct drives pumps and auxiliary equipment. The geothermal reservoir fluid directly contacts the outer diameter of the tubular reactor and can be drawn off through 2215 and 2216 streams for mineralization recovery through a demineralization unit (DMIN). The bottom hole temperature can exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).

FIG. 23 lists a casing contained reactor configuration with external injection line 2314, casing contained/internal geothermal reservoir fluid isolation and heat transfer line 2313, casing contained/internal tubular reactor 2319, and external geothermal reservoir fluid return line 2316. Geothermal reservoir fluid is injected 2314 and flows downhole and into the reservoir 2310 and through the fracked rock 2309 and flows back out through the return pipe 2311 into the organic rankine unit 2316, which direct drives pumps and auxiliary equipment. The geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through 2313 and 2316 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between FIG. 23 and prior FIGS. 21 and 22 is the use of a hot heat transfer pipe 2307 to isolate the hot geothermal reservoir fluids from the reactor to prevent scaling/fouling on the reactor's wall. The primary enabling benefit of 2307 is to provide easy maintenance/pigging through the inner diameter to remove scale and increase heat transfer. The working heat transfer fluid 2303 transfer heat into the tubular reactor by wetting both tubular reactor and hot heat transfer geothermal pipe. The bottom hole temperature can exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).

FIG. 24 lists a casing contained reactor configuration with external injection line 2414, casing contained/internal geothermal reservoir fluid isolation and heat transfer line 2413, casing contained/internal tubular reactor 2419, and external geothermal reservoir fluid return line 2416. Geothermal reservoir fluid is injected in 2414 and flows downhole and into the reservoir 2410 and through the fracked rock 2409 and flows back out through the return pipe 2411 into the organic rankine unit 2416, which direct drives pumps and auxiliary equipment. The geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through 2413 and 2416 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between FIG. 24 and prior FIGS. 21 and 22 is the use of a hot heat transfer pipe 2407 to isolate the hot geothermal reservoir fluids from the reactor to prevent scaling/fouling on the reactor's wall. The primary enabling benefit of 2407 is to provide easy maintenance/pigging through the inner diameter to remove scale and increase heat transfer. The working heat transfer fluid 2403 transfer heat into the tubular reactor by wetting both tubular reactor and hot heat transfer geothermal pipe. The secondary key difference between FIG. 24 and FIG. 23 is the use of a continuously stirred rod set to force convection downhole to increase heat transfer rate. The bottom hole temperature can exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).

FIG. 25 lists a casing contained reactor configuration with external injection line 2514, casing contained/internal geothermal reservoir fluid isolation and heat transfer line 2513, casing contained/internal tubular reactor 2519, and external geothermal reservoir fluid return line 2516. Geothermal reservoir fluid is injected in 2514 and flows downhole and into the reservoir 2510 and through the fracked rock 2509 and flows back out through the return pipe 2511 into the organic rankine unit 2516, which direct drives pumps and auxiliary equipment. The geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through 2513 and 2516 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between FIG. 25 and prior FIG. 24 are the use of piezo particles to transform stress, generated by gravity acting on the downhole column of circulating heat transfer fluid, into electrical current and heat. Additionally, catalyst can be circulated within the tubular reactor along with piezo particles. The bottom hole temperature can exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).

FIG. 26 lists a casing contained reactor configuration with external injection line 2614, casing contained/internal geothermal reservoir fluid isolation and heat transfer line 2613, casing contained/internal tubular reactor 2619, and external geothermal reservoir fluid return line 2616. Geothermal reservoir fluid is injected in 2614 and flows downhole and into the reservoir 2610 and through the fracked rock 2609 and flows back out through the return pipe 2611 into the organic rankine unit 2616, which direct drives pumps and auxiliary equipment. The geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through 2613 and 2616 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between FIG. 26 and prior FIG. 25 is the use of gas that is adiabatically compressed to release latent heat within the tubular reactor and working heat transfer fluid isolated from the geothermal reservoir. The bottom hole temperature can exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).

FIG. 27 highlights the use of one or more tubular reactor inlets 2704 and outlets 2706 and hot geothermal pipes within the cemented casing 2710. It is important to note that the fully cemented casing acts as a great insulator by reducing heat loss.

The hot heat transfer pipe(s) shown in 2607 can be pigged with a dissolving pig that never returns. Plastic/rubber will depolymerize within the hot tubular and dissolve the pig over time. Thus, the pig never returns once it is injected into the underground subsurface reactor's hot geothermal pipe, because it dissolves due to the high temperature and pressure.

FIG. 28 provides one embodiment, where an Organic Rankine Cycle (ORC) 2800 featuring production pumps (P) 2802 installed in production wells (PW) 2804 that pump hot geothermal fluid from underground into a heat to work conversion system to direct drive centrifuges (C) 2806 and generate electricity (G) 2808 to run lights and equipment in algae farm closed or open cultivation system. The geothermal fluid (5) 2810 indirectly heats a working fluid, such as iso-butane, iso-pentane or other organic fluid, which is heated through the use of a preheater (PH) 2812 and evaporator (E) 2814. The cool geothermal fluid (6) then exits the preheater (PH) 2812 and is re-injected (recycled) into the reservoir and is routed to the algae cultivation system for water makeup. The hot (super-heated) working fluid (1) leaving the evaporator (E) 2814 then passes through control valves and into a turbine (T) 2816 to generate work, which drives a shaft and gear boxes connected to centrifuges (C) 2806 and generators (G) for dewatering algae and biomass. A recycle gas stream 2818 can be present. The working fluid (2) then exits the turbine and enters an air cooled condenser system (ACC) 2820 to lower the temperature. Then the cool working fluid (3) is pumped (sub-cooled) with cool working fluid pumps (CP) 2822 and recycled back (4) to the closed loop exchanger system, where it gets re-heated by geothermal fluid to generate more work.

EXAMPLES

Examples and methods of use are described herein as a basis for teaching one skilled in the art to employ the disclosure in any appropriate manner. These examples disclosed herein are not to be interpreted as limiting.

Example 1

One embodiment to test the system can comprise a bench top scale version of reactor comprised of a larger diameter pipe containing one pump-around, oil/gas/water separator, one tubular reactor and auxiliary temperature and pressure instrumentation. The reactor will be vertically installed and bottom (bottom-hole) rests inside of a heater. The heater is used to simulate geothermal temperature source. Effluent pump-around will be cooled through condenser and recycled back to injection pump for recycle in pump-around circuit. The tubular reactor source tank will contain a select type of organic material in water with an option for catalyst addition. The tubular reactor will inject the biomass laden water into the reactor's annular space, react downhole and flow out into a sample chamber with in-line analyzer. The pump-around discharge will be controlled with a back-pressure control valve. The tubular reactor discharge will be controlled with a back-pressure control valve.

Example 2

One embodiment to test the system will initially inventory the tubular reactor and pump-around with a fixed quantity of deionized water (DI), start circulation on the pump-around. Then turn on the heater and start condenser cooling fluid flow and adjust accordingly. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor injection of aqueous organic material will begin. Once the aqueous organic material injection has completed, a known quantity of DI will flush the tubular reactor. After the flush, then the tubular reactor's effluent DI will begin to be recycled into the inlet. Then the heater will be turned-off. Once the heat transfer fluid temperature in the pump-around system reaches ambient temperature, then the tubular reactor injection pump will be turned-off. Then the pump-around injection pump and condenser cooling fluid will be turned-off. The bench top equipment should be depressurized to ambient conditions prior to opening any chambers, vessels, reactors, piping or tubing.

Example 3

One embodiment to test the system will initially inventory the tubular reactor and pump-around with a fixed quantity of deionized water (DI), start circulation on the pump-around. Then turn on the heater and start condenser cooling fluid flow and adjust accordingly. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor injection of aqueous organic material will begin. The tubular reactor's effluent products will be routed to an oil/gas/water separator. The water will be recycled and mixed with new organic feedstock and water. The oil and gas will be analyzed. Upon determining the steady-state test completion a known quantity of DI will flush the tubular reactor. After flush then start recycling the tubular reactor's effluent DI into the inlet. Then the heater will be turned-off. Once heat transfer fluid temperature in the pump-around system reaches ambient temperature then the tubular reactor injection pump will be turned-off. Then the pump-around injection pump and condenser cooling fluid will be turned-off. The bench top equipment should be depressurized to ambient conditions prior to opening any chambers, vessels, reactors, piping or tubing.

Example 4

One embodiment to test the system comprises a heater capable of discharge temperatures in excess of 400° C., condensing unit, a reactor as described in this application, oil/gas/water separator, injection pump for pump-around circuit and downhole pump for tubular reactor effluent discharge along with associated auxiliary temperature, pressure and flow instrumentation and gauges. The reactor is comprised of a larger diameter pipe containing one pump-around and one tubular reactor. The reactor will be vertically installed and bottom (bottom-hole) rests inside of a heater. The heater is used to simulate geothermal temperature source. Effluent pump-around will be cooled through condenser and recycled back to injection pump for recycle in pump-around circuit. The tubular reactor source tank will contain a select type of organic material in water with an option for catalyst addition. The tubular reactor will inject the biomass laden water into the reactor's annular space, react downhole and flow out into an oil/water/gas separator. The separated water will be recycled to a water storage tank. The oil will be routed to an oil storage tank. The gas will be stored, combusted or vented to atmosphere. The pump-around discharge will be controlled with a back-pressure control valve. The tubular reactor discharge will be controlled with a back-pressure control valve.

Example 5

One embodiment to test the system will initially inventory the tubular reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around. Then turn on the heater and start condenser cooling fluid flow and adjust accordingly. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor injection of aqueous organic material will begin. The tubular reactor's effluent products will be routed to an oil/gas/water separator. The water will be recycled and mixed with new organic feedstock and water. The separated oil will be routed to a storage vessel and gas will be stored, analyzed and vented. Depending upon environmental regulations the gas can require combustion or incineration prior to analysis. Upon completing the steady-state test the tubular reactor will be flushed with treated water. Then turn-off heater. Once heat transfer fluid temperature in the pump-around system reaches ambient temperature then turn-off the tubular reactor injection pump. Then turn-off the pump-around injection pump and condenser cooling fluid. The unit should be depressurized to ambient conditions prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Example 6

One embodiment of the disclosure comprises completing siting study, drilling appropriate exploration holes underground, drilling a tubular reactor underground, installing casing, cementing, fracking bottom-hole rock, hydrothermal spalling of downhole rock to increase surface area, permeability and porosity, tubular pump-around(s), packers to stabilize downhole tubulars, tubular reactor(s) and associated downhole instrumentation, pumps and gauges. Then an organic rankine cycle (ORC) unit will be installed above ground and piped-up to the underground subsurface reactor pump-around tubular(s) and lined-up to pump-around injection pump(s) and associated power equipment. Then the tubular reactor(s) inlet(s) will be fitted to organic feedstock in adjacent algae farm and other opportunity organic waste streams. The tubular reactor(s) effluents will be piped-up to oil/gas/water separation equipment and vessels.

Example 7

One embodiment of the disclosure will initially inventory the tubular reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, and kick-start and pressurize the pump-around system. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity. Adequate condenser cooling fluid flow can be maintained and adjusted accordingly. The cooling fluids can be sourced from algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. The gas, primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactors will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. The tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Example 8

One embodiment of the disclosure will initially inject geothermal fluid downhole into an injection line, inside of the casing, into fracked hot dry rock (HDR). The hot geothermal fluid will then flow through fracked rock back into the casing's annular space between the injection line, reactor and casing I.D. then to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a second hole and casing that will power an organic rankine unit (ORC) with effluent hot geothermal reservoir fluid, so that the fluid remains hot prior to entry into the ORC cycle. The reactor's tubular pump-around system will be inventoried with a fixed quantity of treated water, circulation started using a separate startup pump. After the tubular pump-around system has been circulating then start injecting geothermal fluid downhole to. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and line up to generate electricity. Generated electricity can come from turbine and piezoelectric/thermal devices. ORC condenser cooling fluid flow will be adjusted accordingly. The cooling fluids can be sourced from fin fans or algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes, as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator, downstream bio-oil stabilization unit using ionic separation driven by an applied voltage differential by either ORC electricity or piezoelectric/thermal underground (rods) will further separate light from heavy and also provide opportunity to run downstream catalysis. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. The gas, primarily comprised of carbon dioxide and methane, will be combusted with produced CO₂ used to carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When the injection pipe or effluent hot geothermal reservoir fluid pipe requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and isolated. The tubular reactor effluent will be slowly lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off, isolated and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, pulling pipe, making trips, removing vessels, reactors, piping or coiled tubing.

Example 9

One embodiment of the disclosure will initially inject geothermal fluid downhole into an injection line, inside of the casing, into fracked hot dry rock (HDR). The hot geothermal fluid will then flow through fracked rock back into the casing's annular space between the injection line, reactor and casing I.D. then to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a second hole and casing that will power an organic rankine unit (ORC) with effluent hot geothermal reservoir fluid, so that the fluid remains hot prior to entry into the ORC cycle. The reactor's tubular pump-around system will be inventoried with a fixed quantity of treated water, circulation started using a separate startup pump. After the tubular pump-around system has been circulating then start injecting geothermal fluid downhole to. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and line up to generate electricity. Generated electricity can come from turbine and piezoelectric/thermal devices. ORC condenser cooling fluid flow will be adjusted accordingly. The cooling fluids can be sourced from fin fans or algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes, as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator, downstream bio-oil stabilization unit using ionic separation driven by an applied voltage differential by either ORC electricity or piezoelectric/thermal underground (rods) will further separate light from heavy and also provide opportunity to run downstream catalysis. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. The gas, primarily comprised of carbon dioxide and methane, will be combusted with produced CO₂ used to carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When the injection pipe or effluent hot geothermal reservoir fluid pipe requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and isolated. The tubular reactor effluent will be slowly lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off, isolated and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, pulling pipe, making trips, removing vessels, reactors, piping or coiled tubing.

Example 10

One embodiment of the disclosure will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process. Then inject water downhole into an injection line, outside of the casing, into fracked hot dry rock (HDR). The water will then flow through fracked rock into the casing, through the inner diameter of heat pipes and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, and kick-start and pressurize the pump-around system. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity. Adequate condenser cooling fluid flow can be maintained and adjusted accordingly. The cooling fluids can be sourced from algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. The gas, primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. The tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Example 11

One embodiment of the disclosure will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process. Then inject water downhole into an injection line outside of the casing, into fracked hot dry rock (HDR). The water will then flow through fracked rock into the casing and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, start stir rod agitation and kick-start and pressurize the pump-around system. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity. Adequate condenser cooling fluid flow can be maintained and adjusted accordingly. The cooling fluids can be sourced from algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. The gas, primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactors will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. The tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off, stir rod turned off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Example 12

One embodiment of the disclosure will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process and containing piezothermal/piezoelectric particles to generate current and heat when stressed by hydraulic force. Then inject water downhole through fracked rock into the casing and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, start stir rod agitation and kick-start and pressurize the pump-around system. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity. Adequate condenser cooling fluid flow can be maintained and adjusted accordingly. The cooling fluids can be sourced from algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. Post processing of bio-oil/crude oil leaving The underground subsurface reactor to be separated into light, distillate and heavy fractions prior to shipment. Oil stabilization to be accomplished by using an underground geothermal density and ionic separation unit that uses geothermal heat to drive density separation and ionic separation by bridging geothermal with piezo-electric rods that generate a voltage drop across the separation fluid due to the temperature gradient inside of the underground separation column. Thus, the column uses geothermal energy for heat and for ionic separation processes. Using density separation alone is not ‘cost-effective’ due to time constraints (current practice in my yellow grease tanks, goes slower during winter and faster during summer)—however, ionic separation is also used to speed-up separation processes, which is typically driven by an applied electrical voltage. The gas, primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. The tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off, stir rod turned off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Example 13

One embodiment of the disclosure will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process and containing piezothermal/piezoelectric particles to generate current and heat when stressed by hydraulic force. Then inject water downhole through fracked rock into the casing and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, start stir rod agitation and kick-start and pressurize the pump-around system. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and line up to generate electricity. Adequate condenser cooling fluid flow can be maintained and adjusted accordingly. The cooling fluids can be sourced from algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin. The tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator. The hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth. The separated oil will be routed to a storage vessel. The gas, primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. The tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off, stir rod turned off and depressurized. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Example 14

In an embodiment of the disclosure, a super-critical fluid is injected into a capillary injector manifold and an organic material is injected through a tubular reactor injector. An injection capillary can be accessed from the top of the well head. The capillary tubes are present within the tubular as is the organic material. The fluid and material travels down through the downhole casing. The organic material is turned into hydrocarbons due to high temperature and high pressure. The hydrocarbon can then be cracked into various components including but not limited to light ends and heavy ends.

Example 15

One embodiment of the disclosure is super-critical fluid injectors within the tubular reactor. Fluid is heated under pressure at the surface and is injected into the capillary tubes inside of the tubulars to hydrogenate, hydrolyze, and crack the hydrocarbons in the tubular reactor. Direct liquefaction causes the hydrocarbon to crack into light components. Insulation can be used around the tubular or capillary injectors. The insulation can be selected from the group including but not limited to ceramic, kaowool, and gas.

Example 16

In one embodiment of the disclosure FIG. 3 an algal Feedstock 302, will be injected. Carbon Dioxide will be recycled to cultivate and boost productivity. In Item 3.2, a Super critical fluid (SCF) 304 will be injected. The SCF will be comprised of water, hydrogen, alcohol, and organic. In Item 3.3, a Catalyst 306 comprised of pyrite, sulfur, iron, cobalt, sodium, salts, metals, carboxylic acids, and rare earths will be injected. In Item 3.4, a Heat exchanger 308 preheats feedstock, the feedstock 302 (Item 3.1) can bypass based upon operational mode and heat demands. Additionally, if required feedstock can be ran through heater 312 (Item 3.6). In Item 3.5, a Heat exchanger 310 will preheat the SCF (Item 3.2). In Item 3.6, a Heater 312 will be used to heat solvent and/or feedstock and/or catalyst. In Item 3.7, an Underground Reactor 314 will be used to convert feedstock 302 (Item 3.1) into liquid oil and gas hydrocarbons, with the use of combination with SCF 304 (Item 3.2), catalyst 306 (Item 3.3), carbon-monoxide, and hydrogen transfer solvent (Item 3.8). A Solvent Regenerator 316 will receive the recovered spent hydrogen transfer solvent tetraline, from (Item 3.9) separator 318 to hydrogenate the dehydrogenated solvent with hydrogen, methane and/or di-hydrogen sulfide before injection into underground reactor 314 (Item 3.7). In Item 3.9, the Separator 318 will receive the underground reactor effluent (Item 3.7) and separate out liquid hydrocarbons, solvent, gas (condensable and non-condensable), solids and unconverted feedstock for downstream processing or recycle. In Item 3.10, the Liquid oil product 320 will include hydrocarbon, synthetic crude oil with API 0 . . . 70. In Item 3.11, a Turbine 322 will be a direct drive to pumps for reactor system to move feedstock, SCF, solvent, catalyst and product to generate electricity with a generator. In Item 3.12, the Refinery or Plant 324 will receive converted hydrocarbon oil product and produce fuels, chemicals and other salable products from the source hydrocarbon and balance of plant processes.

It is noted that terms like “preferably,” “commonly,” and “typically” are not utilized herein to limit the scope of the claimed disclosure or to imply that certain features are critical, essential, or even important to the structure or function of the claimed disclosure. Rather, these terms are merely intended to highlight alternative or additional features that can or cannot be utilized in a particular embodiment of the present disclosure.

Detailed descriptions of one or more embodiments are provided herein. It is to be understood, however, that the present disclosure can be embodied in various forms. Therefore, specific details disclosed herein (even if designated as preferred or advantageous) are not to be interpreted as limiting, but rather are to be used as a basis for the claims and as a representative basis for teaching one skilled in the art to employ the present disclosure in any appropriate manner.

A number of embodiments have been described. Nevertheless it will be understood that various modifications can be made without departing from the spirit and scope of the disclosure. Accordingly, other embodiments are included as part of the disclosure and can be encompassed by the attached claims. Furthermore, the foregoing description of various embodiments does not necessarily imply exclusion. For example, “some” embodiments, “exemplary” embodiments, or “other” embodiments can include all or part of “some,” “other,” and “further” embodiments within the scope of this disclosure.

All of the compositions and methods disclosed and claimed herein can be made and executed without undue experimentation in light of the present disclosure. While the compositions and methods of this invention have been described in terms of preferred embodiments, it will be apparent to those of skill in the art that variations can be applied to the compositions and methods and in the steps or in the sequence of steps of the methods described herein without departing from the concept, spirit and scope of the invention. More specifically, it will be apparent that certain agents which are both chemically and physiologically related can be substituted for the agents described herein while the same or similar results would be achieved. All such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the spirit, scope and concept of the invention as defined by the appended claims. 

What is claimed is:
 1. An underground reactor for use in creating fuel from organic material, comprising: a first conduit that injects an organic material underground; a second conduit that collects reacted organic material produced by the underground reactor; a heat exchanger for extracting heat; a biomass source; and concentrating equipment that separates the biomass from its cultivation medium.
 2. The underground reactor of claim 1, further comprising a plurality of capillary injection tubes.
 3. The underground reactor of claim 1, wherein the heat exchanger is used for powering equipment used in the creation process of a substance selected from the group consisting of oil and fuel.
 4. The underground reactor of claim 1, wherein the concentrating equipment is a centrifuge.
 5. The underground reactor of claim 1, further comprising an expander powered by geothermal energy.
 6. The underground reactor of claim 5, wherein the expander is a turbine.
 7. The underground reactor of claim 5, wherein the expander powers the concentrating equipment.
 8. The underground reactor of claim 1, wherein the biomass source is a biomass farm that grows the organic material.
 9. An underground reactor for use in creating hydrocarbons from organic material, comprising: a first conduit that injects an organic material underground; a second conduit that collects reacted organic material produced by the underground reactor; and a heat exchanger for extracting heat; wherein the organic material is pulverized coal.
 10. The underground reactor claim 9, further comprising a plurality of capillary injection tubes.
 11. The method of claim 9, wherein the heat exchanger is used for powering equipment used in the fuel creation process.
 12. A method of performing a high-pressure, high-temperature reaction comprising: (a) sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, and chemicals; (b) bringing the compound selected from the group consisting of fuel, hydrocarbon, and chemicals up through a second conduit; (c) using a heat exchanger for extracting heat; and (d) sending geothermal fluid to a biomass growth.
 13. The method of claim 12, wherein the geothermal fluid comprises carbonates and biocarbonates.
 14. The method of claim 12 further comprising injecting super-critical fluid through capillary tubes in the first conduit.
 15. The method of claim 12, wherein the heat exchanger is used for powering equipment used to convert the organic material to a compound selected from the group consisting of fuel, hydrocarbon, or chemicals.
 16. The method of claim 12, further comprising adjusting pressure by a method selected from the group consisting of increasing tubular reactor depth, decreasing tubular reactor depth, increasing back pressure at surface, decreasing back pressure at surface, and loading the tubular reactor working fluid with high specific gravity material mixed within the working fluid. 